SA01220564B1 - Oil refining - Google Patents

Abstract

Abstract: The oil refining method of the present invention comprises a fractional distillation process 1 for distillation and separation of the feed oil into a distillate and a residue (M2), a hydrorefining process (2) in which at least one portion of the distillate (Ml) is repeated by hydrogenation The desulfilrized sulfur is separated, thus obtaining a refined oil by hydrogenation ((M3 hydrorefined oil), the deasphalting process with a solvent (3), where the asphalt is separated from the precipitate (M2) by a solvent, thus obtaining an asphalt-free oil (M4) as an extract and two M5 (asphaltene) as a residual residue, the process of separating metals and sulfur by hydrogenation 4 hydrodemetalizating/desulfurizing, where the demetalized metals are separated from at least one part of the asphalt-free oil (M4) and the sulfur is separated by hydrogenation, thus obtaining refined HDMS oil, and a first mixing process where one part is mixed on less than refined oil (M3), and thus we get benzene products.

Description

Oil refining method Full description

Invention background

The present invention is concerned with a method for refining osmolar oil to produce a number of petroleum products of high value and with high efficiency. More specifically, to the method of refining petroleum (oil) to produce a number of high-value products that have specification

© Variable and high potency than food heavy oil or oil with a low percentage of

Sulfur (Sulfur «80150].

The 8 technologies of this type known in the first field include the following technologies, which are qualified to effectively obtain petroleum products and intermediate products used for the production of analogues;

(1) 1 Technology for the production of thermally distilled gasoline and gas oil by separating feed oil into a distillate and atmospheric residue through atmospheric distillation; distillation of the atmospheric precipitate into air and treatment of the atmospheric precipitate VR) in a coker oven; and

(Y) A technique for the use of an asphalt separation solvent (SDA) for atmospheric sludge and an oil application

0 free of asphalt (DAO) to be obtained as a feed for the FCC process; Or use vacuum distillation (VDU) of the atmospheric precipitate and use vacuum gaseous oil (VGO) and thus obtain it as feed for the fluid catalytic distillation (FCC) process.

anyway; The technology number 1 previously described faces the problem where the bottom of the coker furnace is compressed by adding superstructure, which hinders the construction of productive furnaces.

.byproduct of coke as a by-product 0

Tech No.? Previously described has the same problem as described below. Fuel such as gasoline and gaseous oil can be produced by separating Cu) free from asphaltene and vacuum gaseous oil from heavy crude faa 0.7

. Has a large amount of reserves or air residual and for which an additional source is expected in the future; Treatment of asphalt-free oil or vacuum gaseous oil by means of a fluid catalytic cracking (FCC) process or a hydrocracking (HCR) process. However, this scheme will cause an imbalance in the need for an electric source for the increasing need 0 for gasoline and gas oil, which is expected globally. In addition to Techniques 1 and 7; previously described; There is a specific technology for producing gas turbine fuel (GTF) from very heavy crude which has a higher percentage of vanadium (V) or from atmospheric residue through Adee asphalt separation by solvent. anyway ; The technology has the same problem, where productivity increases (extraction rate 0) production of asphalt-free oil in the process of separating asphaltene by a solvent, which leads to higher pollution than an asphalt-free oil product by means of atomization metals and/or precipitated carbon This results in a processing load (press lel; LHSV low) during the refining of asphalt-free oil by separation of minerals and sulfur, thus making this method economically indistinguishable When productivity is reduced From an oil product to 0 _ of asphalt in order to avoid the previously described problem; the productivity of gas turbine fuel is reduced in order to avoid the previously described problem; and the productivity of the produced gas turbine fuel is reduced; which leads to a new problem for the increased production of asphaltene, which has an additional value The present invention, Gag, provides a method for refining an oil to obtain 0 - petroleum products (eg Je gas turbine fuel) having a vanadium content of 00+ ppm wt or less and intermediate petroleum products therein A metallic content (VAN) of Vo equal to ppm weight or less that can be effectively used as a feed for a FCC or HCR process at the same time; Whereas heavy feed oil or feed oil with particularly low Yo sulfur content can be used as starting material.

General description of the invention: The petroleum refining method according to the first objective of the present invention represents a method for producing petroleum products containing a number of intermediate petroleum products by refining feed oil ¢ including a phi fractional (differential) process to separate the feed oil © into a distillate dropper precipitate during distillation; glee hydrocracking, where at least part of the distillate obtained from the fractional distillation process is refined and desulfurized sulfur is separated by hydrogenation in the presence of hydrogen and a catalyst, and thus Jan asphaltene-free oil as an extract with asphaltene as a residual precipitate; The process of hydrogenation and separation of metals and sulfur in which, 0.0, the metals and sulfur of at least one part of an asphalt-free oil are separated by hydrogenation in the presence of hydrogen and a catalyst, thus obtaining refined oil 170118 from which the metals and sulfur have been separated; And the preliminary blending process Cus that one part of the refined oil and at least one part of the hydrorefined oil are blended to obtain one of the petroleum products EP Vo for the following refining method; And since a part of the refined hydrorefined oil is mixed with a part of the refined HDMS oil in the initial blending process, it is therefore possible to obtain petroleum products with sufficient Jl content of vanadium (V) For example gas turbine fuel and also for the production of intermediate petroleum products with a relatively low metal content (VAN) which can be used as feed for the process of 0 catalytic distillation (FCC) or hydrocracking (HOR) process from The remaining amount of HDMS refined oil where the intermediate petroleum product is used as a feed for the fluid catalytic distillation process or the hydrocracking process has a softer tolerance of metallic contents than Sle turbine fuel or the like; Therefore, the yield of deasphalted oil, Yo, originates from a solvent-based asphalt separation process and can be optimized for gas turbine fuel and feed for a fluid catalytic distillation or hydrocracking process in Ed.

0 at the same time; Thus, suppressing the asphalt productivity from the aquifer residue 811100306112 A gas refining method according to the second objective of the present invention, which includes a distillation process functional to separate the oil feed from the distillate © and the remaining through Ale distillation; Hydrorefining process whereby at least one part of the distillate obtained from the fractional distillation process is La pS and sulfur separation is carried out by hydrogenation and in the presence of hydrogen and a catalyst, thus obtaining refined hydrogenated oil; Asphalt separation process using a solvent, where the asphalt is separated from the residue by a solvent in order to obtain an asphalt-free oil as an extract (pitch) 0 as a precipitate; Hydrodemetalization / desulfurization process, where at least one part of the asphalt-free oil is separated from the metals and sulfur through a hydrogenation process and in the presence of hydrogen and a catalyst, thus obtaining HDMS oil that is free of metals and sulfur ; Cus vacuum fractional distillation process Refined HDMS 0 oil is vacuum distilled and separated into vacuum gaseous oil and atmospheric precipitate; Second Blending Process Cus that at least one part of vacuum gas oil and at least one part of hydrorefined oil are blended to obtain a petroleum product. According to the previously described refining method 0 and where at least one part of vacuum gaseous oil and at least one part of hydrogenated refined oil are mixed 0 with the second mixing process ¢ and it is possible to obtain petroleum products with a low content of AUS of vanadium (V) For example, La . Gas turbine It is possible to obtain intermediate products from petroleum with a relatively low metallic content (VND), which can be used as feed for the process of fluid catalytic distillation or hydrocracking from the residue of this petroleum gas or the atmospheric residue obtained by Yo atmospheric distillation; Even from Cu) repeater HDMS

1a Also, and where of HDMS refined oil is subjected to the vacuum distillation process in order to separate into atmospheric gaseous oil and atmospheric precipitate with low metallic content and residual carbon content by using a range of boiling points for the characteristics of the diy distillation, especially in the process of vacuum distillation; Relatively high concentrations of vanadium© and metals allow HDMS refined oil; This improves the yield of asphaltene-free oil for the solvent-based asphalt separation process. Therefore, asphaltene production can be suppressed from the aquifer residue.

A method according to the third objective of the present invention comprising a fractional distillation process to separate the feed oil into a dropper and a precipitate remaining through the distillation process; Hydrogenation refining process where at least one part of the distillate obtained from the fractional distillation process is refined and the sulfur is separated from it by hydrogenation and in the presence of hydrogen and a catalyst to obtain hydrogenated oil; a vacuum fractional distillation process where the precipitate is distilled in a vacuum and separated into a vacuum gaseous oil and a vacuum precipitate; A solvent-based asphalt separation process in which the asphalt is separated from the vacuum precipitate with a solvent, thus obtaining free Cu fe 01 asphalt as the extract and asphaltene as the residual precipitate; HYDROGENATION / HYDROSULPHATION PROCESS WHERE THE VACUUM GAS OIL AND ASPHALTH-FREE OIL ARE COMBINED AND THE MIXER IS SUBJECTED TO HYDROGENATION / HYDROSULPHATION PROCESS IN THE PRESENCE OF HYDROGEN AND A CATALYST Thus obtaining a refined HDMS oil from which the metal and sulfur have been separated; and a third blending process where at least 1 part Yo of Refined Oil 110145 and at least 1 part of Hydrogenated Oil are blended with such

Obtain a petroleum product. According to the current refining method; and where at least one part refined oil and at least one part hydrogenated oil are blended in the third blending process; Thus, the vanadium content of the blended and collected oil is sufficiently reduced, and it is possible to obtain a petroleum product to be used as a gas turbine fuel. It is also possible to obtain an intermediate petroleum product with a relatively low metal content (VND), which can

9.1

It is not used as feed for a fluid catalytic distillation process or hydrocracking of the remaining refined oil obtained by treating the mixture of vacuum gaseous oil and asphalt-free oil from the hydrogenation process, as the product The petroleum medium used as feed for the fluid catalytic distillation process or hydrocracking has a variable concentration of metallic contents than that in turbine fuel or the like, so the yield of asphalt-free oil in the solvent-based asphalt separation process can be improved from By producing turbine gas fuel and feeding to a fluid catalytic distillation process or hydrocracking at the same time, thus suppressing the production of asphaltene from the atmospheric residue. or less, so the quantity of asphaltene produced can be made less than the first field, as a large amount of asphaltene containing low commodity value arises as a by-product, and therefore improves the productivity of a number of petroleum products with high additional values; Thus, a significant improvement in productivity (Productivity vo) creates a method for petroleum refining according to the fourth objective of the present invention. It represents a method for producing petroleum products, including a number of intermediate petroleum products, by refining (Cy) feed containing a low sulfur content; It includes a fractional distillation process to separate the feed oil into dropper and residue during the distillation process; Fractional distillation separation process to separate the feed oil into dropper and residual during the distillation process; Separation process of YS asphalt with a solvent Since the precipitate obtained from the fractional distillation process, the asphalt aie is separated by a solvent, thus obtaining asphalt-free oil as an extract and asphaltene as a residual precipitate; The process of separating metals and sulfur by hydrogenation, whereby at least one part of the asphalt-free oil is separated from the metals and sulfur through the hydrogenation process and in the presence of hydrogen and a catalyst to obtain refined oil from which YO has previously separated sulfur and metals from it; A fourth mixing process in which one part 0.7 is mixed

A

at least from the refined oil and at least one part of the distillate thus obtaining a petroleum product. According to the current method of refining; and where one part of the refined oil and at least one part of the hydrogenated oil are blended in a fourth blending process; Therefore, it is possible to obtain a petroleum product with a small amount of gas turbine, for example, gas turbine fuel can be obtained from an intermediate petroleum product with Lad. (V) Vanadium is sufficiently low in metallic content, which can be used as a feed for a fluid catalytic distillation process or a hydrocracking process from the residue of refined oil. Whereas, the intermediate petroleum product used as a feed for a fluid catalytic distillation process or Hydrocracking has a higher tolerance for more varying concentrations of metallic content than 0 for a gas turbine fuel or the like; Therefore, the yield of asphalt-free oil produced from the solvent-based asphalt separation process can be improved by producing turbine fuel at the same time as hydrocracking and feeding to a fluid catalytic distillation or hydrocracking process; Thus, the production of asphaltene from the atmospheric precipitate is suppressed. An oil refining method according to the fifth objective of the present invention, which includes a ro fractional distillation process to separate a feed oil into a dropper and a residual precipitate through the distillation process; A solvent-based asphalt separation process in which the precipitate obtained in the fractional distillation process is separated from the asphalt with a solvent, thus obtaining hydrodemetalizating asphalt-free oil as an extract and two asphalts as a residue; The process of separating metals by hydrogenation is that at least one part Cus hydrogenation by hydrogenation desulfurizing sulfur separation - 0 from asphalt-free oil, the metals and sulfur are separated from it by hydrogenation in the presence of hydrogen and a catalyst, thus obtaining refined oil free of Metals and sulfur; a vacuum fractional distillation process whereby the refined oil is distilled in a vacuum and separated into a vacuum gaseous oil and a vacuum residue; And a fifth blending process whereby at least one part .of vacuum gaseous oil and at least one part of the dropper are blended in order to obtain YO petroleum products.

a for that refining method; and where at least one part vacuum gaseous oil and at least one part dropper are in the fifth blending process; Therefore, it is possible to obtain a petroleum product with a sufficiently low vanadium content, for example, as turbine fuel. It is possible to produce an intermediate petroleum product with a relatively low metal content (VANI) and be used as a feed for a fluid catalytic distillation or hydrocracking process from the vacuum gaseous oil residue or the liquified gaseous residue from the vacuum distillation process; and even from refined oil 110148. Also; The refined oil is subjected to vacuum distillation so that it is separated into gaseous oil and a vacuum residual precipitate with low metal content and low residual carbon content 0 by using a range of boiling points for distillation characteristics, especially in the vacuum fractional distillation process; Thus, it obtains relatively high concentrations of vanadium and metals, which are allowed for refined oil; This improves the asphalt-free oil yield in the solvent asphalt separation process; Therefore, the production of asphaltene from the atmospheric deposit can be suppressed. eo An oil refining method according to objective VI of the present invention comprising a fractional distillation process to separate the feed oil into a dropper and a precipitate through distillation; Vacuum Fractional Distillation Process Since the precipitate obtained in the fractional distillation process is vacuum distilled and separated into a vacuum gaseous oil and a vacuum precipitate; A solvent-based asphalt separation process whereby the asphalt is separated from the vacuum oil with a solvent, thus obtaining an asphalt-free oil “0” as an extract and asphaltene as a precipitate; The process of separating metals and sulfur by hydrogenation, where the vacuum gaseous oil and the oil (Jal) from the asphalt are mixed, and the metals and sulfur are separated from the mixture by hydrogenation in the presence of hydrogen and a catalyst, thus obtaining a refined oil free of metals and sulfur; A sixth blending process where one part of refined oil and at least one part of distillate are mixed thus obtaining one of the petroleum products, Ye.

Ye

HDMS according to this refining method; Where one part of the refined oil and at least one part of the dropper are blended in the sixth blending process; The vanadium content of the blended oil becomes sufficiently low and a petroleum product can be obtained that can be used as a gas turbine fuel. also ; It is possible to obtain an intermediate petroleum product with a sufficiently low metallic content that can be used as a feedstock for a fluid catalytic distillation © or hydrocracking process even from a residual refined oil obtained from the treatment / mixture of vacuum gaseous oil and free oil Asphalt in the process of separating metals from sulfur by hydrogenation. Where the intermediate oily product can be used as feed for the catalytic distillation process, it is of high concentration hydrocracking or fluid catalytic fluid 0 for turbine gas fuel or the like; Le variance of yield metallurgical contents of the asphalt-free produced oil in the solvent asphalt separation process can be improved by producing turbine gas fuel and feeding to the process of fluid catalytic distillation or hydrocracking at the same time; Thus the production of asphaltene from the vacuum precipitate is suppressed. According to the present invention of oil 1 when a method of objective 1- is used; to vo or less; The amount of asphaltene Logs 1 can be made to have a low sulfur content equal to pla, the yield is lower, as for the first field, since a large amount of asphaltene containing a low commodity value; This improves the productivity of petroleum products that contain high additional values. This results in a significant improvement in productivity. Brief description of the drawings: Ye Flow of process diagrams representing Diagrams 1 to Fig. 1 Fig. No. - to + of the petroleum refining method according to Invention 1 of AB shows the current. Flow of process diagrams representing 11 digrams to Figure No. 1 Figure No. 6 to 1 shows gas refining methods for test examples from Yo 7.77

11

Detailed description:

Now proposed examples of petroleum refining method according to the present invention will be described. Below with reference to the accompanying graphics. anyway ; It is understood that the present invention will not be limited to the examples described below; For example ; No compatibility

© Components of these examples are intended to be fuel within the intent of the present invention.

Figure No. 1 is a process flow diagram showing an example of a petroleum refining method according to the present invention; Where heavy crude oil is used as feed oil, which produces turbine gas fuel (017), feed for the fluid catalytic distillation process (FCC) and feed for the hydrocracking process (HOR) at the same time.

1 There is no specification of the oil feed to be processed; Any hydrocarbon oil can be used, from crude oil to heavy oil. The following description will deal with cases where the present invention is applied to heavy crude oil, for example, Orinico Tar, and especially to heavy oils with a gravitational degree APT not exceeding Yo, which occurs tli Us gale to improve productivity to obtain a number of Petroleum products containing values

0 extra high.

Gravity APT is an index for classifying crude oils by their physical properties and is estimated from the specific gravity in the following equation, where 8 is specific gravity at 01 degrees Fahrenheit. API- ) 141.5/ 8-5

0 according to the method of this example and where the previously described heavy crude oil is used as the feed oil; The feed oil is first subjected to a fractional distillation 1 to separate it into a MI dropper consisting of low-boiling oil and 1/2-boiling-point precipitate Ale by distillation similar to the first field. while the upper parts; Ally commonly used air distiller; It is preferably used as a fractional distillation apparatus for this

Yes example; There is no specification for the device and the means of distillation (sell). Distillations can be extracted cumulatively without classification, or extracted separately after classification by boiling point.

a

VY

Distillates are extracted in a number of categories, and some categories of distillates are suitable for “hydrorefining” the requirements of petroleum specifications; Hydrorefining process 11. It can be neglected or bypassed as shown by the arrow, and then at least part of the distillate 141 obtained in the distillation process in order to be refined and separate the sulfur from 1 is introduced to the fractional 1 hydrorefining process 0 and a catalyst; Thus, hydrogen oils are produced by hydrogenation in the presence of hydrogen. 113 refined by hydrogenation 143 and in the hydrogen refining process of Qattara 141; Hydrogen gas mixed with

NiMo dropper 1141 and the mixture enters into a reactor filled with catalyst 00140 or catalyst Ml containing in dropper nitrogen and sulfur where the sulfur contents Ye are separated by hydrogenation in the presence of hydrogen at high pressure; Then followed by separating hydrogen gas in a high-pressure separator, thus obtaining hydrogenated oils M3' 113 and hydrorefined oils.

M2, the precipitate oY, regardless of the hydrogen refining process with an asphaltene solvent, enters the asphalt separation process 1 obtained from the fractional distillation process 1 in order to separate the asphalt with a solvent; Thus obtaining an asphalt-free oil (SDA) (M5 process as an extract and two M4 asphalts (DAO dle) in contact with the M2 solvent in the solvent asphalt separation process; the precipitate is placed in a countercurrent flow in Extraction tower with solvent and separating into asphalt-free oil The oil is extracted Alle and asphalt containing metals and carbon precipitated in concentrations of 0 free asphalt together by a solvent through the upper top of the tower, and the solvent is separated from the extracted material in a high critical condition The asphaltine is extracted together with the solvent through the bottom of the tower, and the solvent in the extracted material is separated by evaporation. Example: sulfur, vanadium, Ju contained in asphalt-free oil at 7.77

VY

precipitated nitrogen and carbon. According to the present invention; The extraction ratio of the vanadium content contained in the asphalt-free oil to the vanadium content contained in the feed oil is preferably set to be 770 when the precipitate is used as Usa atmospheric oil as the feed oil; or within 710 when the distilled precipitate is used as feed. 0 The extraction ratio can be chosen in each case; The extraction rate ranges according to the type of feed oil and the vanadium content. In the case of a precipitate obtained by fractional distillation of a low-sulfur feed oil containing a sulfur content equal to or less by weight # and used as feed oil; The vanadium content contained in free oil ppm wt. when distilled YO asphalt precipitate is used is set within 0 ppm wt. when distilled YO 71 ppm precipitate is used as feed oil; or airborne as feed oil. According to the present invention; It can produce refined oil with an effective ratio. maximum extraction in a solvent-based asphalt process; without placing a characteristic load on the hydrometallurgical / sulfur separation process that follows the solvent asphalt separation process; In all 1 of the previously described cases. In the case of the refining process following the asphalt solvent separation process, it includes only the hydrometallurgical / sulfur process; ; It is preferable to adjust the extraction rate of the solvent asphalt separation process © so that the extraction rate of the vanadium contained in the used oil M2 included in the asphalt-free (V) precipitate 144 to the vanadium content Ye as feed oil is 770 or less. At least one part of the asphalt-free oil 144 obtained from the solvent asphalt process is used to the hydrometallurgy/sulfur process; ; Where the minerals and sulfur are separated from the asphalt-free oil (HDMS) process by hydrogenation in the presence of hydrogen and a catalyst, thus obtaining YO 90.1 oil

8 bis free of metals and sulfur. The process of separating metals / sulfur by hydrogenation is similar to process No. Already described ¢ and its description will be deleted. Metal and sulfur separation conditions are chosen for the refined oil 110145 ((M6) obtained in the process of metal / sulfur separation by hydrogenation. So that the content of 0 vanadium is equal to 1 ppm weight or less; 1 ppm weight is preferred. or less; preferably a sulfur content of #0 wt.7 or less; preferably 70.2 or less. Hence, one part of the HDMS Refined Oil (146) obtained from the hydrogenation process; and at least one part of the hydrorefined oil 0 1043 obtained from the refining process by hydrogenation 1 and they are mixed in the first blending process 0 and thus obtain a petroleum product.In order to obtain gas turbine fuel (GTF) as a petroleum product obtained from the blending process © the mixing conditions are adjusted so that the content of Vanadium for refined oil is assumed to be equal to 1 ppm wt; for example, the ratio of 0 refined oil to hydrogenated oil is 1 : 1 or less (where the lower ratio of refined oil is 110148( 146)) by volume For blending, as the vanadium content in the hydrogenated oil is equal to zero ppm weight of the oil 110145 refined 146 obtained from the process of separating sulfur and metals by hydrogenation; ; The remainder that is not exposed to the first mixing process © is used as an intermediate petroleum product, Ye €; And the rest that is not exposed to the first mixing process © and is used as an intermediate petroleum product used as feed for the fluid catalytic distillation process (FCC) the hydrogen cracking process (HOR). of hydrogenated oil '143 eg naphtha tis; gasoline ¢ kerosine or <u) .oil gas according to the present refining method previously described; and where at least one part Ye of refined oil and at least one part of hydrogenated oil are blended; From vo it is possible to obtain a petroleum product with a low vanadium content US ¢ eg turbine fuel. It is also possible to produce an intermediate petroleum product with low oil content, Lani (7+0), which can be used as feed for the fluid catalytic distillation process or the hydrocracking process; From the remainder of HDMS refined oil, 0 number of petroleum products with high added value can be produced at the same time. Where the intermediate petroleum product is used as a feed for a fluid catalytic distillation process or a hydrocracking process with a higher tolerance of metal content concentrations either to 017 turbine gas fuel or the like; Therefore, the yield of asphalt-free oil 144 produced from a no-load solvent-based asphalt separation process of dee 0 sulfur hydrogenation can be improved; This suppresses the production of asphaltene 145 from the remaining sludge

M2 now with reference to Diargam process flow in Figure 1; And in the case of asphalt-free oil obtained from the solvent-based asphalt separation process? It contains relatively any concentrations of metals and sulfur; and blended with a portion of refined oil which ALS has feed properties for a fluid catalytic distillation or hydrocracking process and is 1 satisfactory; A derived portion may be sent via a secondary route indicated by reference No. 11 in Figure 1 to be mixed with a portion of the refined oil; Instead of exposing it to the process of separating metals and sulfur by hydrogenation; ; Thus obtaining intermediate petroleum products used as a feed batch for a fluid catalytic cracking (FCC) process or a feed batch for a hydrocracking (HCR) process 0 (second embodiment) Figure ¥ represents a sequence diagram explaining the second embodiment of the petroleum refining method according to the invention Present ; Where gas turbine fuel (617) and feed for the hydrocracking process are produced at the same moment from the feed oil; By analogy with the first embodiment shown © in Figure .1

The second embodiment differs from the first shown in Figure 1 mainly in that the process of fractional distillation by vacuum 7 is added to follow the process of demineralization / desulfurization; ; In order to treat the purified petroleum 110145 m1 that resulted from vacuum distillation and separate it into vacuum gaseous petroleum Va and vacuum residue Aa through Adee vacuum distillation. In other words, 0 -; Using the petroleum purification method shown in Figure No. ; The resulting 1 O 685 purified petroleum is distilled similarly as in Example No. shown in Figure 1 in vacuum in the vacuum fractional distillation process 1. And in the vacuum fractional distillation process; The HDMS purified petroleum enters into a vacuum distillation tower where the HDMS purified petroleum is distilled and separated into a component with a low boiling point and another with a high boiling point; While the discharge gas, Vo, which has a low boiling point, is produced from the top of the tower, and the remaining M, which has a high boiling point, is produced from the bottom of the tower. Due to the use of the previously described vacuum fractional distillation process 0, the extraction ratio of the vanadium content present in the asphalt petroleum removed fa to the 10 vanadium (V) content present in the residue Ya used as feed petroleum is about 790 or less. This makes it possible to improve the production of petroleum products without the signature of a heavy hydrometallurgical/desulfurization process. The conditions for demineralization and desulfurization of the selected petroleum 110145 m 1 resulting from the process of hydrometallurgy / desulfurization of the deasphalted petroleum m4 are chosen in order to control the vanadium content of the purified petroleum 110145 m up to 01 ppm weight. 01 ppm or less is preferred; Desirably control the sulfur content to 5 wt. or less; 70.7 wt. or less is recommended. Furthermore ; It is required that we control the vanadium content in the vacuum distillation petroleum of the selected petroleum Ta HDMS to 1 ppm Yee wt or less. .to

Lvl and after the aforementioned operation; At least part of the vacuum gas petroleum, Va, produced in the vacuum fractional distillation process 7, and at least part of the aqueous purified petroleum, Ya, produced in the hydropurification process ¥, are mixed in the second mixing process 1, thus obtaining a petroleum product. In order to produce gas turbine fuel (GTF) with the petroleum product resulting from the second mixing © process, the mixing conditions are adjusted to achieve a vanadium content of 8.8 ppm or less, similar to the example shown in Figure 1. And in that case; Correctly adjust the mixing ratio according to the vanadium content in the discharge gas petroleum, in accordance with the previous example. and when the vanadium (V) content in the discharge gas petroleum, Va, is 0 ppm wt# or less; It may be used as a gaseous fuel for the turbine without adding 0-m purified petroleum to it. The rest of the petroleum is used as the discharge gas, Va; and the rest of the discharge, Aa, produced by vacuum distillation; And the rest of the purified petroleum HDMS M1 that is not paid for the vacuum fractional distillation process 1 independently or in a suitable combination thereof, and thus we present an intermediate petroleum product that is used as a feed charge for the fluid catalytic cracking process (FCO) or a lead feed charge 1 hydrocracking ( 010. By using the aforementioned petroleum purification method, the purified petroleum oY 110145 Te is subjected to vacuum distillation and separated into the vacuum gas petroleum Va and the vacuum residue Aa which does not have any appreciable metal content or residual carbon content using Range of boiling points for distillation properties in the vacuum fractional distillation process 7 Relatively high concentrations 0 of vanadium may allow metals and residual carbon to be present in HDMS M1 purified petroleum itself, thus improving the production of deasphalted petroleum M in the solvent asphalt removal process? Therefore, we can inhibit the production of asphaltene (pitch m©) from the remaining Yo, and with regard to petroleum deasphalted oil M4 resulting in the process of removing asphaltene with the solvent ¥; also in da that The vanadium content in Yo m is so low that part of the m may enter; for sub-track 11 to be mixed with the rest of the dump

Ya

From being subjected to a process of removing Ya; Thus, intermediate petroleum products are produced that are used as a feed charge for the fluid catalytic cracking or as a feed charge for the hydrocracking process. The product in the Vo HDMS process can also include the introduction of purified petroleum sent from the fractional distillation process, Ap, to a mixture with the rest of the discharge 11?; In the sub-path 0 by vacuum 6, thus producing intermediate petroleum products that are used as feed batch for the fluid catalytic cracking or hydro-fracking process. (The third embodiment) Figure No.? a sequence diagram explaining the third embodiment of the present invention; where Jia and the feed charge for the fluid catalytic cracking process (GTF) gaseous fuel produced for the turbine Ve

Jill at the same time of petroleum; By symmetry with (HCR) or hydrocracking (FCC). Vacuum Fractional Distillation Process 1 Fractional Distillation Petroleum Gas 11 C Vacuum and Residual Vacuum 1 M Vacuum Distillation; By removing 0

Va where the remainder of the discharge M11 separates into asphalt-removed petroleum YY solvent-removed asphalt / (asphalt) by solvent-removing asphalt; As well as the process of hydrometallurgy VE, asphalt, and petroleum gas We subject the asphalt-removed petroleum mixture Cua YY vacuum desulfurization M11 to a hydrometallurgy / desulphurization process, and thus we produce purified petroleum

NO. HDMS 0 11 m and using the petroleum distillation method shown in Figure No. “; The residue is distilled by vacuum in the fractional distillation process 1 with the example shown in Figure No. BL The resulting 01. is vacuum distilled in the distillation tower Ya residue Jay and in the vacuum fractional distillation process; it is separated into A low-boiling component and a high-boiling component Yo are vacuum-dried where the residual Yo is distilled off

Boiling while the discharge gas M11 oil with a low boiling point is coming from the top of the tower and we get the rest of the discharge (VY) with a higher boiling point from the bottom of the tower. And after the vacuum fractional distillation process, Yo; The remainder of the resulting Wa discharge is subjected to a solvent removal asphalt process 71 and separated into M1 removed asphalt petroleum and CV a © asphalt, although the process of solvent removal asphalt is identical to that in the examples shown in Figure 1 and 7 ; It is desirable that Jay is the upper limit of the vanadium extraction ratio of the M1 asphalted petroleum produced from the discharge residue by the aq-l solvent asphalting process in analogy with the metal concentrations; and residual carbon and sulfur which are higher than those in residual Ya ; Therefore, the extraction rate is better controlled by about 01 Jo, then the M1 asphalt removal oil is mixed with the resulting M11 vacuum gas oil, and the mixture is subjected to a hydrometallurgy / desulfurization process; Thus, we obtain petroleum HDMS (dial M51). It is advisable to choose the conditions for demineralization and purified sulfur removal 5M01 resulting in order to achieve a vanadium content? ppm weight or less; preferably 1 ppm weight or less; and sulfur content 16 0 ppm wt. or less, preferably 0.7 ppm wt. The aqueous purified petroleum (Yo) produced in the water purification process 1 in a third LK process YY, thus obtaining gaseous fuel for the turbine as one of the petroleum products with a vanadium (V) content of 159 ppm ppm Of the 110148 m 1 purified petroleum produced by the hydrometallurgy/desulphurization process YY the residue not subject to the third mixing process YY may be used as an intermediate petroleum product to be driven into the FCC or fracturing process aqueous (0108.i) case of M1 asphalt-removed petroleum and M11 vacuum gas petroleum Yo comprise wildly different concentrations of minerals; residual carbon and sulfur and require conditions

XY. partial hydrogen; which differ greatly from each other; bia interaction; especially from confusion; The hydrometallurgy/desulphurization process in Yau 1 M may be subjected to M 11 and M 11 independent reactors all under optimal conditions; Then mixes, or at least mixes a part of the M11 discharge gas petroleum subjected to the hydrometallurgy / desulfurization process, and at least the one in which (GTF) Ag ill is part of the aqueous purified petroleum M" and that we get gaseous fuel © Vanadium content of #40 by ppm or less. According to the petroleum purification method described before, because part of the purified petroleum and at least part of the aqueous purified petroleum are mixed in the third mixing process 1138

Janie; The vanadium content in the resulting petroleum mixture becomes very low; YY can be made on gaseous fuel for the turbine as one of the petroleum products. It is also possible that we will obtain an intermediate petroleum product with a very low metal content (00 + 1), which may be used as a feed charge for the catalytic cracking of fluids or the hydrocracking process, even from the rest of the pure petroleum.

Vo Petroleum removed asphalt Va resulting from the discharge gas petroleum mixture Yo. HDMS Desulfurization; Therefore, the Lobe group of products can be produced by a high additive metal removal process at the same time. Its petroleum daddy No The intermediate petroleum product used as a feed charge for the catalytic cracking process oY for fluids or hydrocracking has high acceptable concentrations of metal contents of concentrations in Wo gas turbine fuel or the like; Oil production may be improved by asphalt removal by producing gas turbine fuel and feed charge YY solvent removal asphalt process for fluid catalytic cracking or hydrocracking at the same time; In doing so, we inhibit the production of Yo

Yo of discharge residue asphaltene (pitch) 1414 1m Asphalt The fourth through sixth embodiments that may apply preferably when low sulfur crude is used as feed petroleum will be described later. In this description, the example of Arabian light feed oil, the low-sulphur crude, indicates Iranian light crude oil. Marianne; And other crude oil that has a sulfur content of 5

YY

l or less than those of the previous samples ¢, especially crude oil (Blan) with a concentration of .77.0 by weight or less, which includes a sulfur content, which is in the first embodiment and which deals with (HT) and the aqueous purification process is canceled (The process with heavy crude oil is from the following embodiments because the crude used is low sulfur. In other considerations, basically the same operations as those in the first embodiment are 0 by adding the letter A to the end of the reference number used in the first embodiment.) The fourth embodiment) represents the shape of a number, a sequence diagram showing the fourth embodiment of this invention.In the fourth embodiment, the aforementioned low-sulfur crude is used as feed oil, which is subjected to a fractional distillation process 1a and distilled similarly as in the old methods to separate into product 0 It has a higher boiling point Ya Distillate M1a is composed of low-boiling petroleum with a residue and a device similar to the one in the first embodiment can be used into IY products and the resulting M1 distillate is separated in the fractional distillation process

Ne distillation of Ma; m” by a scintillation unit, the product in the fractional distillation process 1a using IY, and the bottom residue is removed on Jani petroleum; Thus, IY (SDA) is a solvent in the solvent removal asphalt process (Process

Joa as extractor as well as asphalt (Pitch) (DAO) Ifa solvent asphalt removed in TY and in solvent asphalt removal process; First, the residual, in a reverse flow inside the extraction tower, comes into contact with the solvent and is separated into asphalt-removed petroleum and asphalt (asphalt) containing metal and residual carbon in high concentrations. The petroleum is removed from the asphalt in addition to the solvent, through the top of the tower; The solvent is separated from the extracted material in a critical - super stage. In addition to the solvent, the asphalt is extracted through the bottom of the tower. The solvent in the extracted material is removed by evaporation. In the event that the purification process following the asphalt removal process with solvent “A” only includes the hydrometallurgy / desulfurization process; A; We'd better control Yo

YY

The ratio of solvent asphalt removal process so that the vanadium content of the asphalt-removed petroleum is M © ppm weight or less. With solvent “a” to the process of hydrometallurgy / desulfurization (process A; so that the metal of the petroleum part is removed from the asphalt and its sulfur is removed by hydrogenating it in the presence of 0 hydrogen and a catalyst, and therefore we obtain purified petroleum 110348 m 1 whose metal was removed and desulfurized. And because the hydrometallurgy/desulfurization process is essentially like the heavy metal described by feed oil; the hydrometallurgical process that deals with crude oil, and its explanation will be omitted. on HDMS M1 refining petroleum having a vanadium (V) content of 7 wt ppm or less; preferably 1 wt ppm or less; and a sulfur content of 70.5 wt or less; 70.7 preferably By weight or less, and a part of the purified petroleum 110345 m 1 produced in the process of 0 - hydrometallurgy / desulfurization a is mixed with at least part of the distillate m “baa” in the fourth mixing process fo and thus we get a petroleum product . In order to produce du all gaseous fuel as a petroleum product produced in the fourth mixing process, co, the mixing ratios are adjusted so as to achieve a vanadium content of #,© by weight of ppm or less in the petroleum product. And if the vanadium content in the distillate petroleum is 1 Ma HDMS ud 0 ppm wt and the vanadium content in the distillate m?a is zero ppm wt; Sia; The ratio of HDMS purified petroleum m1 to distillate fre is set at 1 : 1 or less (i.e. a smaller percentage of 110148 ms of refined petroleum and of 110148 ms of HDMS purified petroleum produced in the hydrometallurgy process). / Yo desulfurization a; the remainder of it not subjected to the fourth mixing process (fo) is used as an aphid product

YY

. (HCA) or hydrocracking (FCC) is an intermediate petroleum that pays for the catalytic cracking process of the fluid and the remaining aqueously purified petroleum m? ; Which did not undergo the first mixing process (a) may be used as a petroleum product, such as naphtha; gasoline; Kerosene or gaseous petroleum. According to the previously described petroleum purification method; Because the purified ppm and at least a part of the aqueous purified petroleum m?a are mixed; It is possible that we will get Na HDMS 0 . Jie gas turbine fuel is based on a petroleum product with a low vanadium content (Ni + V). We can also produce an intermediate petroleum product with a relatively low metal content, which may be used as a feed charge for the fluid catalytic cracking or hydrocracking process. ; We efficiently produce a group of petroleum products that have added value 11, (HCA).

Ade 0 and because the intermediate petroleum product used as a feedstock for the fluid catalytic cracking or hydrocracking process has acceptable concentrations of metal contents higher than that of the turbine gas fuel (fea cali wl) or the like; The production of petroleum removed from the solvent A asphalt removal process can be improved without the overload of the hydrometallurgical/desulfurization process; Thus, we discourage the production of asphalt (asphalt) What is left of the m? ; In the event that what is produced in the process of removing asphalt with solvent A includes petroleum asphaltene, the asphalt is removed with relatively low concentrations of minerals and sulfur and mixed with a portion of the purified petroleum that includes lower concentrations of minerals and sulfur in order to meet 98 Requirements for the properties of the feedstock for the fluid catalytic cracking or hydrocracking process; 0 may be sent in the form of a number; meaning 11 is part of it through the sub-path indicated by reference number M; instead of being subjected to the HDMS process by mixing it with part From purified (refined) petroleum, we thus produce an intermediate petroleum product that uses fe hydrometallurgy / desulfurization as a feedstock for the fluid catalytic cracking process or hydrocracking.

A\R4 (Fifth Embodiment) Fig. No. © represents a process sequence diagram explaining the fifth embodiment of the petroleum refining method according to this invention; In it, gas turbine fuel and feed batch for fluid catalytic cracking or hydrocracking are produced at the same time from feed petroleum; 4. By analogy with the embodiment shown in Figure No. ©. This embodiment differs from that shown in Figure No.; Basically we are adding a hydrometallurgical/desulfurization process; a; For BT vacuum fractional distillation, we process purified petroleum 110145 m1a in vacuum distillation and separate it into vacuum gas petroleum

JA MA and discharge residuals

C0 In other words; Using the petroleum refining method shown in Figure No. 1, the output is similar to the example shown in Figure No. 1m HDMS; purified petroleum is distilled

J by vacuum in a vacuum fractional distillation process in HDMS 11 and in a vacuum fractional distillation process; The purified petroleum enters the vacuum distillation tower, where the purified petroleum is distilled 110145 m1! It is separated into a low-boiling component that is lower than the top of the tower, and we obtain the vacuum residue, M0, with a boiling point higher than the bottom of the tower. Because the vacuum fractional distillation process described above is carried out; It is possible to control the percentage of the asphalt-removed petroleum recovery £ 0 produced by the solvent removal asphalt process so that the weight of ppm. and from 50; At Mia, the desired upper limit of vanadium content is set; then the extraction rate can be made higher and the production and extraction of petroleum products can be improved. Hydrometallurgical Process 112 HDMS 01 to achieve a desulfurizing / hydrodemetalizating vanadium content of ppm wt. or less; while, 01 wt. ppm or less; preferably y 7032 sets the sulfur content as desired at 70.9 wt. or less; It is preferable by weight or less. Moreover; It is preferable to adjust the vanadium content in petroleum gas part weight in 1 m1 up to HDMS vacuum distillation of selected petroleum millionth or less. © And after the aforementioned process; At least part of the resulting vacuum gas petroleum A is mixed in the mixing process Iva in the vacuum fractional distillation process 11 and the distillate thus obtaining one of the petroleum products. IV V The petroleum product produced in the Jia process (GTF ) In order to produce gaseous fuel for the turbine, ppm 1.8, the vanadium content is controlled up to IV 0 or less in symmetry with the example shown in the figure; . And in that case; Adjust the mixing ratio. Similar to the previous example, Va according to the vanadium content in the discharge gas petroleum ppm +0 Va, and when the vanadium content of the discharge gas petroleum is or less; This may be used as gaseous fuel for the turbine without adding the distillate M’a. The distillate TAs and the remainder of the discharge gas petroleum is used as M’a; The unpaid remainder of the vacuum HDMS fractional distillation process and the remainder of the purified petroleum by vacuum “A” separately or in a suitable combination thereof as an intermediate petroleum product to be used as a batch feed for the process or hydro-fracking. 1s HDMS and using the aforementioned purification method; Because the purified petroleum is subjected to vacuum distillation in a vacuum fractional distillation process “A” in order to separate into gas 0 which does not include any noticeable metal content and carbon content TAL and the rest of the vacuum IVa is a residual vacuum using a range of boiling points for distillation properties ; The same high concentrations may be allowed; 1 M HDMS is relatively vanadium; Minerals and carbon remaining in purified petroleum improves the production of asphalt-removed petroleum M; in the solvent “A” asphalt removal process; Therefore, .a0m can inhibit the production of asphalt (bitumen) m#a from the residual Yo

AR

The result of the process of removing the bottom with the solvent? significantly reduced; Ala may also be; in

Tha to be mixed with the discharge residue IVY Enter a part of M; in the subpath; instead of being subjected to the removal of 1 sent from the vacuum fractional distillation process _Hydrometallurgy / Desulfurization ;a; To obtain an intermediate petroleum product to be used as a shipment ©

Jal Feed for catalytic fluid cracking or hydrocracking. The product can also be introduced into the hydrometallurgical/desulfurization process A to HDMS purified anil 11, sent from the distillation process Ap to mixture with vacuum residue NY sub-pass vacuum 11 thus producing products An intermediate petroleum used as a feed charge for a fluid catalytic cracking or hydrocracking process. the invention; For the case of producing gaseous fuel for the turbine at the same time from (HOR) or hydrocracking (FCC) of the fluid catalytic cracking process with feed oil; In line with the anthropomorphism shown in Figure 4. This embodiment differs from 1 shown in the form of a number; Basically, the fractional distillation process 1a is followed by the fractional distillation process

Ya discharge M10a and discharge residue Sle into petroleum IY where the residue fre is separated by vacuum TY by vacuum distillation; And the process of removing asphalt with a solvent 17a, where the rest of the discharge and asphalt (asphalt) m?

NY, where the asphalt-removed petroleum mixture IVY hydrometallurgy / desulphurization 0 and vacuum gas oil M11 are subjected to the process of hydrometallurgy / desulfurization, and thus we produce

Vo. 110145 Purified petroleum by using the purification method shown in Figure 6; The remaining M?a product is distilled in the same way as in the example shown in the form of a number; by vacuum in the dy Yo yy vacuum fractional distillation process and in the vacuum fractional distillation process; Enter the remainder m?a the result similarly as a.01 in the example shown in the form of a number; vacuum in the vacuum fractional distillation process and in the vacuum fractional distillation process; The remaining M?a enters a fractional distillation tower where M?a is distilled and separated into a low-boiling component and a high-boiling component; While petroleum is produced by the low-boiling-point M11 vacuum gas from the top of the tower, and the high-boiling-point M11a vacuum gas is extracted from the bottom of the tower.

Try is followed by the vacuum fractional distillation process 10a by the process of removing asphalt with the solvent resulting in the previous process into asphalt-removed petroleum TY Ya, where the vacuum residue is separated, while the vacuum fractional distillation process is similar to the cases Nea and asphalt (asphalt) hy, shown in the form of a number; Figure No. 0 The ratio of the removed asphalt 0 petroleum extraction produced in the process of removing asphalt by solvent in the remainder of the discharge is adjusted so that the desired upper fiva limit of the vanadium content rises; For example, up to 000 ppm weight response that is higher than that Fa for metal concentrations; residual carbon; And the sulfur in the remaining M7a. And the discharged gas oil M11 resulting in 1a. Then the asphalt-removed petroleum is mixed to obtain dl Ty and the mixture is subjected to a hydrometallurgy / desulfurization process; the purified petroleum is 110145 M. And it is preferable to choose conditions for removing metal and sulfur for petroleum? Weigh the resulting ppm (V) to achieve the Yo. HDMS sul ppm or less; a sulfur content of 70.9 wt. or 1 or less; preferably less; It is preferable to have 70.7 by weight or less. 0 Then, part of the purified petroleum 110148 M01 produced in the process of removing the metal is mixed in the sixth mixing process??a in order to obtain Trp water / desulfurization 77 and the distillate to obtain gaseous fuel A gaseous turbine fuel as a petroleum product having a vanadium content ppm or less.‎ 58

Ya

The resulting fou HDMS in the demineralization process, and the remaining water purified oil / desulfurization 7a that was not paid to the sixth mixing process may be used as an intermediate petroleum product to be used as a feed charge for the fluid catalytic cracking or hydrocracking process. The vacuum gas M11a has Ye and in the case of asphalt-removed petroleum, wildly different concentrations of minerals; residual carbon and sulfur and require reaction conditions 0, especially the partial pressure of hydrogen; which differ greatly from one another; may be exposed rather than mixed; For the hydrometallurgy/desulfurization process in separate Pp M A reactors all under optimal conditions; then mix together; Or mix at least a part of the M11 discharge gas petroleum that has undergone a hydrometallurgical / desulfurization process with at least a part of the distillate M, thus obtaining a gaseous turbine fuel that has a content of 0 ppm or million by weight. 0.6 vanadium is because part of the purified petroleum 0 and according to the previously described petroleum purification method and at least part of the distillate are mixed in the sixth mixing process Yo HDMS "A; the vanadium content in the blended petroleum becomes low We can get gaseous fuel for the turbine as one of the petroleum products, and it is also possible that we can produce 0 ba sill products that are used as an intermediate petroleum feedstock (VANE) with a low metal content resulting from the catalytic fluid op HDMS or Hydrocracking even from the rest of the purified petroleum is a mixture of degassed petroleum M “and asphalt-removed petroleum M”1a by hydrometallurgical / desulfurization process. Thus, a group of intermediate petroleum products with high added value can be produced efficiently. Ye and because the intermediate petroleum product used as a feed charge for a fluid catalytic cracking process for mineral contents of a Malis turbine fuel or hydrocracking (0108 has a higher tolerance FCC) a gaseous IVa removal process or the like; The production of asphalt-refined petroleum and GTF feedstock (GTF) with solvent 1?a can be improved by producing asphaltene gas turbine fuel for fluid catalytic cracking or hydrocracking at the same time; Thus, we inhibit the production of Yo.a1"m asphalt (tar) m?1a from the discharge residue

Yq Experimental examples This invention will be described later more specifically through experimental examples (1) Experimental Example No. A group of petroleum products comprising gaseous fuel for the turbine and intermediate petroleum products were produced to be used as feed batch for a fluid catalytic process or Water cracking as 0.1 by means of the oil purification method shown in Figure No. 1 Seen in the form of a Gravity API number (Orinoco oil) Use super heavy crude (Orinoco petroleum) Part weight in YAY vanadium and a sulfur content of 77.17 by weight and a vanadium content of 1) melison as a feed batch which was distilled first under atmospheric pressure (fractional distillation process) and the rate of the product was Yo. and a residue of Vp in the upper part, thus obtaining a distillation product of 0 The distillation m1 was 719.9 by weight of the feed oil, the sulfur content was 77.49 by weight, the residual production rate was 787.5 by weight of the feed oil, while the sulfur content was ppm by weight, and the vanadium content was EV by weight. 24.07 Then, the sulfur was removed from the distillation product, M1, produced in a water purification process, in the presence of Fp as a product - hydrogen and catalyst, in order to obtain water-purified oils M © M. and use 0 petroleum; naphtha Without additional processing mode. The rate of production of water-refined petroleum by weight from the oil entering the feed, and the sulfur content was 70.07 by weight. Yield 717, by weight, of feed oil. ZY m tal for the Yp asphalt removal process and far from the German purification process; the remainder was exposed as a solvent; So we get pentane with the solvent? In a solvent extraction tower using pentane 00. as a 0a residue on the asphalt removed petroleum m; With an extraction ratio of 7765 and asphalt (bitumen) (solvent / m7) in the asphalt removal process with a solvent at Yo and the ratio of the solvent to the residue was adjusted m; 784,9 by weight of crude oil; was cli WY) and the oil production was removed A by weight; The vanadium content was 717 by weight ppm and 77.00 sulfur content by weight of crude oil. 779.7 0p extraction was 714 . The production of asphalt (asphalt) Yo Ed

Ye And the petroleum removed asphalt m?; The product from a reactor filled with hydrometallurgy and hydrodesulphurization catalyst at a ratio of ©: 57 by volume; To obtain petroleum through the process of hydrometallurgy / desulfurization; In the presence of residual Tp HDMS at partial pressure Jeli hydrogen and catalysts. Conditions were controlled. NI [Ave Jail] Joey; And the ratio of hydrogen is 112 to 100 for hydrogen © hr, and the reaction temperature is 70 °C. was / +,0 LHSV low hourly speed; The feed was 759 by weight of crude oil. This is 1a 110115 dial oil production ppm. A sulfur content 70.49 by weight; The vanadium content was, then the selected petroleum was distilled 110848 m 1 produced in a vacuum (distillation process. Filled with vacuum residue m (VGO) to obtain vacuum gas petroleum) 1 fractional vacuum by weight of crude oil; The AYO content was Va and the discharge gas petroleum yield was ppm wt. 07 Sulfur 70:74 wt; The vanadium content was (Yo line process) and all the oil was mixed as discharge gas M7 with water-purified petroleum to produce gaseous fuel for the turbine at a rate of 778 by weight of crude oil; Vanadium 014 wt ppm The remaining vacuum ve used in the vacuum fractional distillation process as a feed charge for a process without additional treatment HCR or FCC hydrocracking fluid catalytic cracking may also be produced. With it is fed to the process of catalytic fracturing of fluids or hydrocracking by mixing part of m1 with the discharge residue HDMS of asphalt-removed petroleum m; or part of purified petroleum by weight of AE The feed batch produced in this way showed a production rate of Ap 0 Weight of 1.7 fraction of crude oil; sulfur content 70.6 by weight and vanadium content per million.

HY (Experimental Example No.) A group of petroleum products comprising gas turbine fuel and intermediate petroleum products has been produced to be used as feedstock for the fluid catalytic cracking process YO

A

and hydrocracking as seen in Figure No. 9 using the petroleum purification method shown in © Figure No. ; And the sulfur content is YA APT and an extra-heavy crude (Arabic Heavy) was used that has gravity by weight and a vanadium content of 14 ppm as a feed oil that was distilled in an upper part to get a product (1) first under atmospheric pressure (fractional distillation process By weight of crude oil was 741 Va, and the distillate yield was Ya 1 m distillate and a residue by weight of petroleum was 7897855 Yo, and the sulfur content was 720.794. The rate of the residue was the weight of a part in 1117 of the crude; while The sulfur content was 0.77, and the vanadium content was 0.1 million, in order to obtain 01, then the resulting residue was subjected to a vacuum fractional distillation process 11 01 C on M11 vacuum gas petroleum and M11 vacuum residue. by weight The crude oil content was 77.917 by weight The sulfur content was 27/7 770.61 ppm The yield of the discharge residue M711 was 0.960 Vanadium Os by weight ppm; YY by weight of crude oil; the vanadium content was 1776.4 ppm wt.; the remaining YE (7+1) carbon content was 0 wt. and the sulfur content was 75.04 wt.; naphtha; kerosene; And the petroleum gas produced from the LPG nag, purification of the aqueous cus sections? (Let's get Aga Alec oils) separately by hydrogenation Vo distillation and the production of petroleum was. Yao Va Corresponding aqueous (aqueous fractions (light fractions) 70.06 _ aqueous purified M” is 770.70 by weight of crude oil by weight. Crude oil was sulfur content; gaseous petroleum was kerosene; and kerosene was gasoline by weight. The production of gasoline was by weight and 717.7 by weight, respectively, of 76 Fa of purified petroleum gas, then feed oil, crude J, and apart from the hydropurification process; the remaining 71 m was subjected to the asphalt removal process in an extraction tower solvent using solvent deasphalting process 21 71 solvent Yo

YY deasphalted oil M13 11m as a solvent ¢ to obtain isobutane deasphalted oil with an extraction rate of 770 and asphalt (asphalt) m1 as a residue. The ratio of the solvent to the residue was controlled and the production of A discharge m1 (solvent / m1) in the process of removing asphalt with solvent at 718.4 by weight of crude oil was 1.13 deasphalted petroleum; deasphalted oil fraction weight In YY the sulfur content was 74.17 by weight; The vanadium content was © 717.7 Vea million and the extraction rate was 719 . The production of asphalt was by weight from crude oil. A mixture of M1 removed asphalt oil and M11 discharge gas oil was introduced into a hydrodemetalizing catalyst reactor filled with hydrodemetallizing catalyst by volume; To obtain petroleum 1: 1 with a hydrodesulfurizing catalyst ratio of 0 through the hydrometallurgical / desulfurization process; In the presence of 05 M HDMS purified 00 hydrogen and catalysts, the process conditions were set at a partial pressure of hydrogen per hour and a degree of 1.7 / 11187 liters. It was [NL Ave. Joey; The ratio of 112 to petroleum by weight is 19 744 C HDMS, the reaction temperature is 76 C. The production of purified petroleum was crude oil; the sulfur content was 70,6 by weight; The vanadium content Ve was ppm. 1 vanadium 10m HDMS Then mixing 715 by weight (attributable to feed oil) from the selected petroleum to obtain gas turbine fuel including an aqueous Yo content (idl produced with petroleum Weight ppm, production rate of 1.47 wt. sulfur 70.78 wt., vanadium content wt. of feed oil and use the remainder, namely ¢ 774 wt. of petroleum 0 240 as a batch for a fluid catalytic cracking or hydrocracking process. Purified HDMS Experimental examples that used crude oil with low sulfur content will now be explained as follows: A group of petroleum products comprising gas turbine fuel and intermediate petroleum products used as feed batch for fluid catalytic cracking and fracturing process has been produced. 4.0 by the method of petroleum purification shown in Figure No. 01 aqueous as seen in Figure No. 7.7

AR

And the use of crude oil with a low sulfur content (Arabic Light) with a sulfur content of 71:79 by weight and a vanadium content of 1,560 ppm as feed oil, which was first distilled under atmospheric pressure (fractional distillation process A1) in an upper part 7 , 0 Ta and a remainder of m?a . The rate of production of the distillate was 1p to obtain a distillate by weight of crude oil, and the sulfur content was 70.17 by weight. And the rate of production of © leftovers M? A was 745.4 by weight of crude oil; While the sulfur content was 77.7 by weight ppm. Tr and the vanadium content on Ja ail products was 0 and the distillate was separated from the resulting M1a in a unit and its past as a petroleum product; naphtha Without additional processing. Vp was a distillery m?a; what . And the use of 70.16 average distillate M?a 8 by weight of crude oil, and the sulfur content Ve was 77.76 by weight of crude oil. Ya by weight. The rate of naphtha and the residue m?a was subjected to a solvent-removal asphalt process *a in a solvent-use tower with an extraction ratio of feo using isobutane as a solvent + to obtain asphalt-removed petroleum as a residue and the solvent-to-residue ratio fo m ( pitch (asphaltene and asphalt 8) and the production of barrels was A (solvent / m ?a) in the process of removing asphalt by solvent at Ya eo is 777805 by weight of crude oil; the sulfur content was fe removed asphalt By weight, the vanadium content is 5.4 by weight of ppm, and the production of asphalt 0 feed (bitumen) was 78 by weight of crude oil, then in a reactor for 4 zl deasphalted oil, the asphalt was removed as Jy, then Insert size 9 : 1 Uke ratio hydrodesulphurization catalyst filled with desulphurization catalyst 0 through the hydrometallurgical / desulfurization process 11, HDMS to obtain purified petroleum and catalysts and controlled process conditions At a pressure of hydrogen in the presence of hydrogen, It 11187 liters, and it was 800 atmospheric / NL, and the ratio of 112 to petroleum was 001 mole hydrogen for 4 “HDMS” hours, and the reaction temperature was 0077 °C. The production of purified petroleum was [0] is “.2776 by weight of crude oil; The sulfur content was 70.1 wt.; and YO content ppm. ad vanadium 7.7

Yes 0

777.7 by weight (proportionate to the product from crude oil) of the resulting 11,HDMS purified petroleum was mixed with the product of the MA distillate (the fourth mixing process (fo), thus obtaining Gaseous Turbine Fuel (GTF) with a sulfur content of 70 44 wt., vanadium content YA wt. ppm 797.76 wt. of crude oil © and use the remainder of the purified petroleum to HDMS, specifically 717.7 wt. Fluid catalyst cracking

(FCC) or hydrocracking (HCR) without additional dallas.

(0 experimental No. Ji)

A group of petroleum products including gas turbine fuel 0 and intermediate petroleum products used as feedstock for the fluid catalytic cracking and hydrocracking process as seen in Figure 11 was produced by the petroleum purification method shown in Figure No. © . He used crude oil with a low sulfur content (Arabic light); It is the same petroleum used in the fourth experimental example; It has a sulfur content of 71.79 wt. Gnas vanadium 1.9 ppm wt. as a feedlot which is first distilled under pressure.

0 atmospheric (fractional distillation process 1a) in an upper part to obtain a distillate Na and a residue IY, the yield of the distillate Ma was 757.50 by weight of crude oil and the sulfur content was 720.17 by weight. The yield of the residue, Ia, was 748.4 by weight of crude oil; While the sulfur content was 77,010 by weight and the vanadium content was Tr by weight ppm.

a The resulting distillate, Pp, was separated into its flash unit, Yo, to obtain distillate M; IP. and the use of the distillate as a petroleum product; naphtha without further processing. The distillate yield was 750.9 by weight of crude oil and the sulfur content was 720.16 by weight. The production of naphtha M? A 7Y,% « naphtha M3A by weight of crude oil.

ve and away from the water purification process; The remaining M?a was subjected to the process A asphalt with the solvent IF in a solvent extraction tower using pentane as a solvent; Let's get oil

Adele

Yo. As residue fo m (pitch) asphaltene with an extraction ratio of 5 and asphalt it removed asphalt mm and the ratio of solvent to purified m?a (solvent / m?a) was adjusted in the process of removing asphalt by solvent

Jail yield is 778.7 by weight of feo and the petroleum production was removed asphalt. A in crude » The sulfur content was 77,850 by weight and the vanadium content was 5.9 ppm by weight of crude oil. 71.8 fog per million. The production of asphalt (asphalt) was © and the petroleum removed asphalt was introduced into a reactor filled with a hydrometallurgical catalyst.

HDMS by size; To obtain purified petroleum 9:1 and desulphurization catalyst by hydrometallurgy/desulfurisation process; a in the presence of hydrogen and 112 atmospheres; The catalyst ratio is 001, and the process conditions are set at a partial pressure of hydrogen

J cll hour and temperature / 1.7 LHSV liter. [NL Ave to petroleum 0 mA was 777.7 wt. of crude oil; HDMS purified petroleum production was SY and the sulfur content was 750/90 wt.; And the vanadium content is 1.0 ppm. IN by vacuum No. 0 production of discharge gas petroleum What is the output is 777 by weight of crude oil and the content was 17 ppm by weight; the vanadium content was 70.010 sulfur and all the discharge gas petroleum was mixed with Aa distillate (5th mixing process 7a) to produce a gaseous turbine fuel having a sulfur content of 70.49 wt and a vanadium content of 00 wt ppm; a production rate of 277.58 wt 0 produced in the fractional distillation process Aa Crude oil and using the vacuum residue without (HOR) by vacuum as a feed batch for FCC or hydrocracking additional processing.The feed batch for FCC or cracking or a fraction of purified petroleum may also produce aqueous Tp By mixing part of the asphalt-removed petroleum, the catalytic cracking process of the fluid, An, with the discharge residue 11 HDMS YO, showed

(FCC) or hydro-cracking rate of production of 71.79 wt. of crude oil; and a sulfur content of 70,16 by weight; TOY vanadium content ppm wt. (Experimental Example No. 6) A group of petroleum products comprising gas turbine fuel 0 and intermediate petroleum products were produced to be used as a feedstock for the fluid catalytic cracking and hydrocracking process as seen in Figure 11 by the petroleum purification method shown in Figure 6. It was used low sulfur crude oil (Arabic light); It is the same petroleum used in the fourth experimental example; It has a sulfur content of 71.79 ppm and a vanadium content of 17.5 ppm wt as a feed batch which is first distilled under 0 atmospheric pressure (fractional phil process 1a) in an upper portion to obtain a distillate of WA and a residue IY, the production of the distillate M1a was 757.5 by weight of the crude Jy ill OSs sulfur content 70.77 by weight and the production of the residue M1a was 745.4 of crude oil; While the sulfur content was 77.01 by weight and the vanadium content was 30.0101 by weight ppm. 'eo', and the resulting residue was distilled by vacuum (vacuum fractional distillation process (I +) to obtain M10 vacuum gas petroleum and a vacuum residue IV Ya. The production of vacuum gas M111 was 770.4 by weight of crude oil; while it was The sulfur content is 77.7 by weight and the vanadium content is 1 wt. The distillate M1a was separated into a flash unit, Wo, to obtain the distillate M1a, IY, and the distillate M1a was used as one of the petroleum products, naphtha, without additional treatment, and the production of the distillate M1a was 290.9 by weight of crude oil, the sulfur content was 75 by weight, and the naphtha production was 77.6 by weight of crude oil.

Yv and away from the water purification process; The discharge residue M?a was subjected to a removal process in a solvent extraction tower using isobutane as a solvent; Let's get YY asphalt with the solvent. As fa residues on asphalt removed petroleum M11a with an extraction rate of 7760 and asphalt (pitfall) and the ratio of the solvent to the discharge residue M (solvent / m "1a) in the process of removing asphalt by weight from oil was 70.9 and the oil production was 70.9 The asphalt was removed as A by solvent at © 1.01 wt crude, the sulfur content was 77,790 by weight, the vanadium content was asphaltene (pitch) M14A 0 ppm. By weight of crude oil d and gaseous petroleum for discharge m11 in Va and a mixture of desalted petroleum entered a reactor filled with hydrometallurgical catalyst and hydrodesulphurization catalyst in a ratio of 1:?0 through the HDMS 110 demineralization process By volume, in order to obtain purified petroleum in the presence of hydrogen and catalysts, the conditions of IYY desulfurization were set at 112 / le. The reaction was 7259 m and the yield was Refined Petroleum | #0 LHSV and the (Te) was 77/854 by weight of crude oil; while the sulfur content was fio. HDMS Ye by weight; and the vanadium content was 54 by weight ppm. And mixed Then that 777.7 L by weight (attributable to crude oil) of petroleum to produce turbine fuel that Ye and thus with the distillate Yo. HDMS il has a sulfur content of 70.49 by weight and a vanadium content of 074 by weight

Jy ial million; At a production rate of 277.6 by weight of crude oil, the remaining 0 was used; Specifically, 779.7 by weight of it as a feed batch for the purified fluid HDMS catalytic cracking process or the hydrocracking process without additional treatment. Industrial applicability The petroleum purification method according to the present invention helps to produce; For example; the weight of part 15 (V) with vanadium content (gas turbine petroleum product (gas turbine fuel) YO 7.7

Ya

31 NIHV per million or less and intermediate petroleum products having a metal content of 1 liter suitable for use as a feed batch in a catalytic cracking process of 1 ppm or less ; From heavy crude oil Orinoco tar (HOR) or hydrocracking process (FCC) for fluid Jow sulfur or as a feed batch with low sulfur content Orinoco F

Claims (1)

Ya protection elements 1-1 Method for purifying petroleum (oil) to produce petroleum products containing SAE products 7 Intermediate petroleum oil by purifying feed oil pla; Including: 0” | Partial distillation process where crude oil is distilled (feed oil) and separated into distillate and residue or ¢ sediment 0 The process of water purification, where at least part of the distillate obtained in a process is purified 1 Partial distillation and sulfur 40 is removed from it by hydrogenation (treatment With hydrogen (hydrogen) the presence of hydrogen and a catalyst, and thus we get + Hydrorefined oil 4 Cus solvent deasphalting process The asphalt of the remaining materials is removed using yy solvent and thus we get deasphalted petroleum as an extractor and asphaltene 1 (pitch tar) as residual materials; 1 The process of removing minerals with water, hydrodemetalizating / removing sulfur Cua desulfurizing VY removes demetalized minerals and desulfurized sulfur, at least part of the petroleum removes asphalt 4 by hydrogenation in the presence of hydrogen and a catalyst Lew catalyst leads to purified petroleum 110115 1 from which the demetalized metals and desulfurized sulfur have been removed; And 1 The first Bla process, where part of the purified petroleum (HDMS) and part of the purified petroleum (Whe av) are mixed, and thus we get one of the petroleum products, oil, where the resulting petroleum product in the first mixing process is gas turbine fuel gas turbine; While the extraction ratio of 14 vanadium content present in deasphalted oil is adjusted to the 0 - vanadium content present in the residue to become 7710 or less in solvent removal asphalt 1; Demineralization and desulfurization conditions for the production of purified petroleum 110145 from vy asphalt-removed petroleum in the hydrometallurgical/desulfurization process are selected to achieve a vanadium content of 7 ppm by weight or less and a sulfur content of 70.50 by weight or less. vs. found in purified petroleum 110145; Crude oil is a heavy oil with an APL vo (American Petroleum Institute) gravity of 710 or less. 1 ?- AAI method Petroleum (oil) according to claim No. 1; where the petroleum product - the product produced in the first mixing process is gaseous fuel for the gas turbine; And the mixing conditions are chosen in » - the first mixing process in order to achieve the vanadium content of 05 ppm by weight; or less in the gaseous fuel of the turbine. 1 *- A method of refining petroleum (oil) of claim No. 1; Where the rest of the petroleum is added » - purified 110145 as an intermediate petroleum product to be used as a feedstock for fluid catalytic cracking (FCC) or »> for hydrocracking (HCR) 1?4- A method for purifying petroleum (oil) to produce petroleum products Containing several intermediate petroleum products by ald petroleum purification; Comprising: » - Cus fractional distillation process Crude petroleum is distilled and separated into distillate and residue or ; - sediment; 0 Water purification process Cus At least part of the distillate product that we obtained in the process > - partial distillation is purified and the sulfur is removed from it by hydrogenation (hydrogen treatment) in the presence of Vv hydrogen and a catalyst, and thus we get water-purified petroleum A: A solvent removal asphalt process where the asphalt of the residual materials is removed using a solvent, thus obtaining q removed asphalt petroleum as an extract and asphaltene (pitch tar) as a residual; a hydrodesulfurization/desulfurization process where the metals are removed and sulfur is at least part 1 -_ of the asphalt-removed petroleum by hydrogenation in the presence of hydrogen and a catalyst which leads to 1 HDMS purified petroleum from which demetalized and desulfurized sulfur has been removed; 10 process Partial vacuum distillation where HDMS purified petroleum is distilled in a vacuum 14 and separated into vacuum gasoil and vacuum residues; and 7.7 yo is a second mixing process where at least part of gaseous petroleum (HAY) is mixed with at least 1x part of water-purified petroleum and thus we obtain a petroleum product, where yy the petroleum product produced in the second mixing process is turbine fuel the gas turbine, while 4A adjusts the extraction ratio of the vanadium content present in deasphalted oil vq to the vanadium content present in the residue to become 770 or less in the cuddly 0 - asphalt removal process Demineralization and desulphurization conditions are selected to produce HDMS vy purified petroleum from Adee asphalted petroleum; By weight or less, yy contained in the purified petroleum 110145; while the vanadium content in the vacuum gaseous petroleum vg resulting from the partial vacuum distillation process is 1 ppm by weight or sedi Yo, the crude oil is a heavy oil for it Gravity according to APT (American Petroleum Institute) 71 or less. 1 #- A method for purifying petroleum (oil (pitch) according to Claim No.; where the petroleum product produced in the second mixing process is gaseous fuel for the gas turbine; and selects the mixing conditions in the second mixing process in order to The vanadium content is 00+ ppm weight, or less than that found in the gaseous fuel of the turbine. Vacuum distillation of purified petroleum 110148 as an intermediate petroleum product + to be used as a feed batch for the catalytic process of fluid cracking or fluid hydrocracking (FCO) ¢ 0 7- A method for purifying petroleum oil (pitch) to produce Petroleum products comprising several intermediate petroleum products by purifying crude oil feed oil; including: £y The partial distillation process where crude petroleum is distilled and separated into distillate and residue or y ; - The sediment; the water purification process, where at least part of the distillate that we obtained in the process 0 is purified (hydrogenation, partial distillation, and the sulfur is removed from it by hydrogenation “1” in the presence of hydrogen and a catalyst 1, and thus we obtain petroleum Hydrogen 7 is a vacuum or vacuum partial distillation process in which the residual petroleum is distilled in a vacuum and separated into A gaseous petroleum 1 H 885 vacuum and a vacuum residue; - Thus, we obtain asphalt-removed petroleum as an extractor and asphalt (tar) as residual materials; 11 where the gaseous petroleum is mixed desulfurizing with water / removing sulfur yy and the resulting mixture removes minerals and sulfur from it 06021160 Vacuum oil and petroleum is removed Asphalt ay which is HDMS by hydrogenation in the presence of hydrogen and catalyst and thus we obtain purified petroleum vg from which minerals and sulfur were removed; and 1 and part of the purified petroleum HDMS a third mixing process where part of the purified petroleum is mixed - Petroleum products, where the resulting petroleum product is in the sal process, and thus we obtain Tle 1, the third mixing of gas turbine fuel; While the extraction ratio of the vanadium content yA to the vanadium content contained in the deasphalted oil contained in the asphalt-residue petroleum is adjusted to be 715 or less in the solvent asphalt removal process; Conditions - 0 are chosen to achieve a vanadium content ¥ HDMS part Demineralization and desulfurization to produce purified petroleum 1 wt or less contained in purified petroleum 720,590 ppm wt or less and sulfur content vy and 5 YY or APT 71 (American Petroleum Institute) Crude oil is a heavy petroleum with a gravity of x less. And choose the gas turbine mixing conditions. The result in the third mixing process is gaseous fuel for the turbine. “in the third mixing process in order to achieve the vanadium content of 08 ppm or less; - Found in the gaseous fuel of the turbine. <1<1 Method of purification of petroleum It (oil) of claim No. 7; Where the rest of “purified petroleum 110145 is added as an intermediate petroleum product to be used as a feedstock for fluid catalytic cracking or + for hydrocracking (0108. -0 1) A method for purifying petroleum (oil) for the production of petroleum products that include several products dds iY L by purifying feed oil pla; including: » - the partial distillation process where crude oil is distilled and separated into a first distillate and a residue or first sediment; © cuddly asphalt removal process where the asphalt of the remaining materials resulting from the distillation process is removed x partial using a solvent and thus obtain deasphalted oil as an extractor and asphalt (tar) as a residual material; A hydrometallurgy / desulphurization 8 where metals and sulfur are removed at least 4 part of the hydrogenated asphalted petroleum in the presence of hydrogen and a catalyst leading to 0 HDMS purified petroleum from which minerals and sulfur have been removed; a flashing process where 1 first distillate is subjected to flashing in order to obtain a second distillate; and 1 fourth mixing process Cus a portion of HDMS purified petroleum and at least part of the product of 1 second distillation, thus obtaining one of the petroleum products; Where the petroleum product 6 produced in the fourth mixing process is gas turbine fuel; while the extraction ratio of vo _ petroleum removed asphalt in the solvent asphalt removal process is adjusted to the vanadium Yo content of 0 ppm by weight or OF ; The conditions for demineralization and desulfurization 1 to produce purified petroleum 8 are selected to achieve a vanadium content of 1 ppm by weight or less A and a sulfur content of 720.90 by weight or less found in purified petroleum 110148; And a Crude oil (feed oil) is a low sulfur crude oil that has a sulfur content x.27 wt. or less. -11-1 A method of purifying this petroleum (oil) according to claim 01; Where the product is » - The petroleum produced in the fourth mixing process is gaseous fuel for the gas turbine; And adjust the mixing conditions in the fourth mixing process in order to achieve the vanadium content 6 ppm wt; - One million or less contained in the gaseous fuel of the turbine. OT Method for Refining Petroleum Oil Tip of Claim No. 01; Where the rest is added » - Purified petroleum 110145 as an intermediate petroleum product to be used as a feedstock for fluid catalytic cracking or ¢ for hydrocracking (HCR) -1-1 Method for purifying petroleum Oil (oil) to produce petroleum products containing several products » - Petroleum intermediates by purifying crude feed oil; Including: »- The partial distillation process where crude oil is distilled and separated into a first distillate and a residue or ; first deposits © cuddly asphalt removal process where the asphalt of the residual materials resulting from the partial x distillation process is removed using a solvent and thus we obtain deasphalted oil as vy extract and asphalt (tar) as residual materials; + hydrometallurgy/desulphurization 8 where minerals and sulfur of at least a part of the petroleum are removed hydrogenated asphalt in the presence of hydrogen and a catalyst 0 resulting in purified petroleum 65 from which the minerals and sulfur have been removed; 11 The partial distillation process by vacuum or vacuum in which the purified petroleum 110148 is distilled in a vacuum 1” and separated into a vacuum gaseous petroleum and a vacuum residue; the flash process in which the first distillate 1” is subjected to a flash to obtain a second distillate; and 7.7 m vg Fifth mixing process Cus At least part of the vacuum gaseous petroleum and at least part vo of the second distillate are mixed, thus obtaining a petroleum product; where is - the petroleum product produced in the fifth mixing process gas turbine fuel; Whereas, pay is set to remove asphalt petroleum in the solvent asphalt removal process so that the vanadium yA content in the asphalt petroleum is 0 ppm by weight or dd and 1 - Demineralization and desulfurization conditions are selected 0018:2108 To produce HDMS 0 purified petroleum to achieve a vanadium content of 01 ppm wt or less and a sulfur content of 70.90 wt 1 or less found in purified petroleum 8 . Whereas, the vanadium content in vy of the vacuum gaseous petroleum produced from the vacuum fractional distillation process is set at 1 ppm vy by weight or less; and ve crude oil is a low sulfur crude petroleum that has a sulfur content of 27 vo by weight or less. -14 1 A method of purifying petroleum (oil) according to Claim 17 wherein the petroleum product x produced in the fifth mixing process is a gas turbine fuel; and select » - mixing conditions in the fifth mixing process to achieve a vanadium content of 0.9 wt ppm; - One million or less contained in the gaseous fuel of the turbine. 1#1 method for purifying petroleum of claim 17; Where the remaining petroleum goal oy vacuum gas oil resulting from the vacuum distillation of residual petroleum 35 is pushed as an intermediate petroleum product to be used as a feed batch for the catalytic process of fluid catalyst cracking or; Hydrocracking - 01 1 A method for purifying petroleum (oil) pitch for the production of petroleum products comprising several intermediate petroleum products by purifying crude oil feed oil; including: The process of partial distillation, where crude oil is distilled, feed oil, and separated into a first distillate; - and residues or first deposits; M Partial distillation process by vacuum or vacuum Cus The residue resulting from the partial distillation process is distilled in a vacuum place and separated into a vacuum gas oil and a vacuum residue; + Cua solvent deasphalting process The asphalt of the remaining vacuum materials 4 is removed using a solvent and thus we obtain deasphalted oil as extract 0 and asphaltene (pitch tar) as residual materials; yy The process of removing minerals with water, hydrodemetalizating, desulfurizing, where yy is mixed with vacuum gaseous petroleum and petroleum removed asphalt and the resulting mixture removes demetalized minerals yy and sulfur 0 by hydrogenation in the presence of hydrogen - 4 and the catalyst, and thus we obtain On HDMS purified petroleum from which metal 1 and sulfur were removed; 0 flashing process where the first distillate is subjected to flashing to obtain a second distillate 10; and 14 sixth mixing process where part of the purified petroleum is mixed HDMS and at least part of the product of gq of the second distillation, and thus we get one of the petroleum products; 0 where the petroleum product produced in the sixth mixing process is the gas turbine fuel; while 1 the oil extraction ratio is adjusted asphalt is removed in the process of removing asphalt the asphalt with the solvent so that the vanadium content present in the petroleum removed asphalt vy becomes part per million by weight or yy less » and the conditions for demineralization and desulfurizing are chosen to produce petroleum vg purified HDMS to achieve a vanadium content of 1 ppm by weight or less and a sulfur content of VO 20.90 by weight or less found in HDMS purified petroleum; The vy crude oil is Yo i feed ol low sulfur crude having a sulfur content of vy 77 by weight or less. 7.7 a -17 0 A method for purifying petroleum (oil, Gig (pitch) of claim 17; wherein the petroleum product produced in the sixth mixing process is gas turbine fuel; + | mixing conditions are selected in the sixth mixing process In order to achieve a vanadium ¢ content of 0.6 ppm wt or less that is present in the gas turbine fuel .gas turbine -18-1 method for refining petroleum in accordance with claim No. 116; Where the remaining x vacuum gaseous petroleum gas oil resulting from the vacuum distillation of purified petroleum 110115 y is paid as an intermediate petroleum product to be used as a feedstock for the catalytic process of fluid cracking or hydrocracking of the fluid.